CN102472572A - Method and apparatus for producing a cooled hydrocarbon stream - Google Patents
Method and apparatus for producing a cooled hydrocarbon stream Download PDFInfo
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- CN102472572A CN102472572A CN201080029190XA CN201080029190A CN102472572A CN 102472572 A CN102472572 A CN 102472572A CN 201080029190X A CN201080029190X A CN 201080029190XA CN 201080029190 A CN201080029190 A CN 201080029190A CN 102472572 A CN102472572 A CN 102472572A
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- stream
- refrigerant
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- hydrocarbon
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 136
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 136
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 134
- 238000000034 method Methods 0.000 title claims abstract description 66
- 239000003507 refrigerant Substances 0.000 claims abstract description 386
- 238000001816 cooling Methods 0.000 claims abstract description 240
- 230000008569 process Effects 0.000 claims abstract description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 113
- 238000007906 compression Methods 0.000 claims description 36
- 230000006835 compression Effects 0.000 claims description 36
- 238000002156 mixing Methods 0.000 claims description 27
- 239000003345 natural gas Substances 0.000 claims description 20
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 9
- 239000001294 propane Substances 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 7
- 238000004886 process control Methods 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims 1
- 239000000203 mixture Substances 0.000 abstract description 20
- 230000001276 controlling effect Effects 0.000 description 18
- 238000009833 condensation Methods 0.000 description 11
- 230000005494 condensation Effects 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 11
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 11
- 239000003949 liquefied natural gas Substances 0.000 description 8
- 238000001704 evaporation Methods 0.000 description 7
- 230000008020 evaporation Effects 0.000 description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- 239000001273 butane Substances 0.000 description 5
- 238000005457 optimization Methods 0.000 description 5
- 230000004044 response Effects 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910001868 water Inorganic materials 0.000 description 5
- 241000282326 Felis catus Species 0.000 description 3
- 230000006399 behavior Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 235000020030 perry Nutrition 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 101100518972 Caenorhabditis elegans pat-6 gene Proteins 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000012797 qualification Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000004590 computer program Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012887 quadratic function Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000006903 response to temperature Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- -1 sulphur compound Chemical class 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0252—Control strategy, e.g. advanced process control or dynamic modeling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B13/00—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion
- G05B13/02—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion electric
- G05B13/04—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion electric involving the use of models or simulators
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B15/00—Systems controlled by a computer
- G05B15/02—Systems controlled by a computer electric
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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Abstract
一种用于生产冷却的烃流(60)的方法和设备。该方法采用在至少两个连续的压力水平下通过在第一和第二换热器(125、145)中使用来自第一混合的冷冻剂流的第一混合冷冻剂的部分而对第一流和第一混合冷冻剂流进行冷却；第一和第二膨胀装置(135、165)；以及用于提供第一混合的冷冻剂流的第一压缩机(105)。冷却过程通过基于模型预测控制的先进的过程控制器而进行控制，从而确定对于一组操控变量的同步控制行为，以便在控制一组控制变量中的至少一个的同时对一组参数中的至少一个参数进行优化。该组操控变量包括：混合的第一冷冻剂的组分；第一膨胀装置(135)的设定；和第二膨胀装置(165)的设定。
A method and apparatus for producing a cooled hydrocarbon stream (60). The method employs cooling a first stream and a first mixed refrigerant stream by using a portion of a first mixed refrigerant from the first mixed refrigerant stream in first and second heat exchangers (125, 145) at at least two consecutive pressure levels; first and second expansion devices (135, 165); and a first compressor (105) for providing the first mixed refrigerant stream. The cooling process is controlled by an advanced process controller based on model predictive control to determine simultaneous control actions for a set of manipulated variables so as to optimize at least one parameter in a set of parameters while controlling at least one of the set of controlled variables. The set of manipulated variables includes: a composition of the mixed first refrigerant; a setting of the first expansion device (135); and a setting of the second expansion device (165).
Description
Technical field
The invention provides a kind of method of producing the hydrocarbon stream of cooling, said method comprises to be cooled off hydrocarbon stream.The present invention also provides a kind of equipment that is used for producing from hydrocarbon stream the hydrocarbon stream of cooling.
Background technology
The common hydrocarbon stream that cools off is a natural gas flow.Such natural gas flow can be cooled to its degree that is liquefied, and in this case, it is commonly called liquefied natural gas (LNG).
There are a lot of reason expectations that natural gas is liquefied.As an instance, natural gas is more prone to store and long-distance transportation as the comparable gas form of liquid, under high pressure stores because it occupies smaller volume and does not need.If this liquefied natural gas is maintained under the cryogenic temperature (such as being in-160 ℃ or following), can under atmospheric pressure, store.
U.S. Pat 6,370,910 disclose the method that a kind of stream that is used for methane rich liquefies.Natural gas flow flows to scrubbing tower, and in this scrubbing tower, heavier hydrocarbon is removed, with the overhead streams (overhead stream) that a kind of gaseous state is provided.From the gaseous overhead stream of column scrubber in the heat exchanger of auxiliary (pre-cooled) by partial condensation.Condensate flow removes from the cat head gaseous flow of partial condensation then, so that the stream of methane rich to be provided.The stream of methane rich then through in the shell-side of main heat exchanger under low pressure the multicomponent refrigerant of evaporation carry out indirect heat exchange and be arranged in the pipe in the main heat exchanger and be liquefied.
The multicomponent refrigerant can be discharged and be compressed from the shell-side of main heat exchanger.The multicomponent refrigerant of compression carries out indirect heat exchange through auxiliary (pre-cooled) multicomponent refrigerant with evaporation under low pressure in the shell-side of supplementary heat exchanger then, and the partly condensation of refrigerant pressure quilt to raise in the pipe in being arranged in auxiliary (pre-cooled) heat exchanger.The multicomponent refrigerant of partial condensation turns back to main heat exchanger then.
U.S. Pat 6; 370; 910 disclose an embodiment; Wherein, the step that the multicomponent refrigerant of compression is carried out partial condensation comprises: through carrying out indirect heat exchange with the auxiliary multicomponent refrigerant that in the shell-side of first supplementary heat exchanger, under middle pressure, evaporates, and with elevated pressure it is cooled off in the pipe in being arranged in first supplementary heat exchanger.Through carrying out indirect heat exchange, be further cooled in the pipe of this multicomponent refrigerant in being arranged in second supplementary heat exchanger then with the auxiliary multicomponent refrigerant that in the shell-side of second supplementary heat exchanger, under low pressure evaporates.
With U.S. Pat 6,370, the problem that 910 liquefaction process is associated is how it to be optimized control, especially about being provided at the layout (line-up) of two supplementary heat exchangers of operation under the different pressures of assisting the multicomponent refrigerant.Have all types of process variables, this process variables can be selected or control, with the cooling procedure in the control supplementary heat exchanger.
Summary of the invention
The invention provides a kind of method of producing the hydrocarbon stream of cooling, said method comprises the cooling to hydrocarbon stream.This method comprises following steps at least:
(a) flow first refrigerant stream that cools off the compression in first-class and the first refrigerant loop through first refrigerant that under first stress level, in first heat exchanger, relies on first expansion; With first refrigerant stream that first refrigerant stream and first first-class, first cooling that cooling is provided warms up, this first refrigerant loop comprises the refrigerant of first mixing;
(b) first to first refrigerant stream of first cooling expands in first expansion gear, so that first first refrigerant stream that expands to be provided;
(c) second portion of first refrigerant stream through in second heat exchanger, relying on second first refrigerant that expand to flow to cool off one or multiply second stream and first cooling; Flow with second stream that provides one or multiply to cool off, first refrigerant that first refrigerant stream and second of further cooling warms up; Wherein, One or multiply second flow to and comprise the first-class of said cooling less and by the first-class attached stream of deriving of said cooling; Hydrocarbon stream is comprised in said one or multiply second stream, so that the hydrocarbon stream of said cooling to be provided at least thus;
(d) in second expansion gear, the first at least of first refrigerant of said further cooling stream is expanded; So that first refrigerant stream of second expansion to be provided; First refrigerant stream of said second expansion is in than under the low pressure of first refrigerant stream of said first expansion, and
The gaseous state of first refrigerant stream that (e) in first compressor, said first first refrigerant stream and said second that warms up is warmed up partly compresses, and then the compressive flow from first compressor is cooled off, and flows with first refrigerant that compression is provided;
Said method also comprises the steps: through using based on the Advanced process control device of Model Predictive Control step (a) to (e) to be controlled; To confirm for one group of Synchronization Control behavior of controlling variable; So that at least one in one group of control variables of control at least one parameter in one group of parameter will optimizing is optimized, controls variable and comprise for wherein said one group:
The component of the refrigerant storage that mix in first in-the first refrigerant loop,
The setting of-the first expansion gear and
The setting of-the second expansion gear,
Wherein said one group of control variables comprises:
One temperature at least in second stream of-said one or multiply cooling,
Temperature difference between at least a in-said first first refrigerant stream that warms up and the following stream: (i) first refrigerant of said compression stream and (ii) said first-class,
Temperature difference between at least a in-said second first refrigerant stream that warms up and the following stream: (i) second portion of first refrigerant stream of said first cooling and (ii) be the first-class of said cooling and/or from said one or the multiply second of the form of the first-class attached stream of deriving of said cooling flows one
In-following the control variables at least one: the temperature difference between first refrigerant stream that the temperature difference between (i) first refrigerant of first refrigerant stream of first cooling and first expansion flows and first refrigerant stream and said second of (ii) said further cooling expand, and
-the power that consumes by first compressor;
And the said one group of parameter that wherein will optimize comprises productivity ratio and/or the cooling effectiveness in the first refrigerant loop of the hydrocarbon stream of cooling.
In yet another aspect, the invention provides a kind of equipment that is used for producing from hydrocarbon stream the hydrocarbon stream of cooling, said equipment comprises:
-the first refrigerant loop, the said first refrigerant loop comprise the refrigerant storage of first mixing; First expansion gear; Second expansion gear; First compressor; With one or more first coolers, said one or more first coolers cool off for the compressive flow from first compressor, thereby first refrigerant stream of compression is provided;
-the first heat exchanger; Said first heat exchanger is arranged and is used under first pressure, relying on first refrigerant of first expansion to flow first refrigerant stream to first-class and compression to cool off; With first refrigerant stream that first refrigerant stream and first first-class, first cooling that cooling is provided warms up, first expansion gear is arranged the first of first refrigerant stream that is used to receive first cooling and first first refrigerant stream that expands is provided;
-the second heat exchanger; Second heat exchanger is arranged and to be used to rely on second first refrigerant stream that expands that the second portion that first refrigerant of one or multiply second stream and first cooling flows is cooled off; Flow with second stream that provides one or multiply to cool off, first refrigerant that first refrigerant stream and second of further cooling warms up; Second expansion gear is arranged the first at least of first refrigerant stream be used to receive further cooling; So that first refrigerant stream of second expansion to be provided; First refrigerant stream of said second expansion is in than under the low pressure of first refrigerant stream of said first expansion; Said one or multiply second flow to and comprise the first-class of said cooling less or by the first-class attached stream that derives of said cooling, and hydrocarbon stream is included in said one or multiply second stream, so that the hydrocarbon stream of said cooling is provided at least thus;
-the first compressor, said first compressor arrange that the gaseous state that is used for first refrigerant that said first first refrigerant stream and said second that warms up warms up flows partly compresses;
-advanced process controller; Said process controller comprises based on the computer-executable code of Model Predictive Control confirms the Synchronization Control effect of controlling variable for one group; So that at least one in one group of control variables of control at least one parameter in one group of parameter will optimizing is optimized; Wherein, control variable and comprise for said one group:
The component of the refrigerant storage that mix in first in-the first refrigerant loop,
The setting of-the first expansion gear and
The setting of-the second expansion gear,
Wherein said one group of control variables comprises:
One temperature at least in second stream of-said one or multiply cooling,
Temperature difference between at least a in-the first first refrigerant stream that warms up and the following stream: (i) first refrigerant of compression stream and (ii) first-class,
Temperature difference between at least a in-the second first refrigerant stream that warms up and the following stream: (i) second portion of first refrigerant stream of first cooling and (ii) be the first-class of cooling and/or flow by one or multiply second of the form of the first-class attached stream of deriving of this cooling in a kind of
In-following the control variables at least one: (i) temperature difference between first refrigerant stream of first refrigerant stream of temperature difference between first refrigerant stream of first refrigerant stream of first cooling and first expansion and (ii) further cooling and second expansion, and
-the power that consumes by first compressor;
And that wherein will optimize one states productivity ratio and/or the cooling effectiveness in the said first refrigerant loop that the group parameter comprises the hydrocarbon stream of said cooling.
Said cooling effectiveness can reflect the relation of the amount of power that As time goes in first compressor, consumes and the cooling hydrocarbon stream of being produced.
Description of drawings
To embodiments of the invention only be described by way of example with reference to appended non-limitative drawings now, in the accompanying drawing:
Fig. 1 is the illustrated scenario according to the method and apparatus that is used for hydrocarbon stream is cooled off of first embodiment; And
Fig. 2 be according to second embodiment be used for hydrocarbon stream is cooled off and the illustrated scenario of the method and apparatus that liquefies;
The specific embodiment
In order to describe the stream that single Reference numeral will be assigned to circuit and in this circuit, transport.Employed same reference numerals identifies same circuit and stream in different accompanying drawings.
Whenever with reference to " low pressure ", " middle pressure " and " high pressure " time; This means and relate to the relative pressure level of this order with respect to other stress levels in the first refrigerant loop.
Such as this use, term " setting " is used for the opening degree of indication equipment (such as valve).Term " is controlled control variables " and is represented that control variables is remained on predetermined value (set point) perhaps to remain in the preset range (setting range).As employed at this, term " is optimized parameter " and is used to instigate parameter maximization or minimizes, and makes parameter be in predetermined value.
Hydrocarbon stream is cooled off preferably as the part of the liquefaction process that is used for hydrocarbon at this disclosed method and apparatus.This cooling procedure is used and is controlled based on the Advanced process control device of Model Predictive Control, so that the productivity ratio of the hydrocarbon stream of cooling and/or the efficient of process of refrigerastion are optimized.The setting of expansion gear is to control variable.
The setting that first mix refrigerant is sent to the expansion gear of first heat exchanger and second heat exchanger controlled make the cooling means optimization.Through changing the setting of expansion gear, the pressure of cold-producing medium between the expansion gear both sides that can handle first mixing changes.This so adjust the variations in temperature of first refrigerant between the expansion gear both sides, thereby make first refrigerant stream cooling can handle expansion first-class with second flow residing temperature.
Model Predictive Control or be a kind of known technology based on the model of Model Predictive Control itself is as in Perry ' s Chemical Engineers ' Handbook, 7
ThEdition, page 8-5to 8-27 (chemical engineers handbook of Perry, the 7th edition, the 8-25 page or leaf is to the 8-27 page or leaf) is disclosed.In U.S. Pat 6,272, in 882; It has been applied in the liquefaction process; This technology to the gaseous state methane rich charging liquefy, obtaining liquiefied product, and the mass flowrate of the mass flowrate of refrigerant part and the stream that will cool off can be used as and controls variable.Warm up temperature difference between terminal and the mid point as control variables, to be used to optimize the output of liquiefied product at main heat exchanger.
U.S. Pat 6,272,882 relate generally to controlling of main heat exchanger, and do not relate to pre-cooled heat exchanger.In U.S. Pat 6; 272; Disclosed Advanced process control principle in 882; Under single pressure, utilized lighter mixed refrigerant part and heavier mixed refrigerant different component and flow velocity partly, this application also is not suitable for as under the different pressures level, the refrigerant that mixes being controlled the situation of the present invention.
Especially, U.S. Pat 6,272,882 with mixed refrigerant than the mass flowrate of light fraction and heavier part as controlling variable.Under present case, it is used for that first-class and second stream are cooled off the mass flowrate that can cause first mixed refrigerant controls.It has been found that the controlling of the mass flowrate of first mixed refrigerant makes the output to the hydrocarbon stream of cooling carry out acceptable optimization.Method of the present invention has been utilized the temperature difference between at least one both sides in first expansion gear and second expansion gear has been controlled, rather than the mass flowrate of refrigerant stream is controlled.
An advantage of the invention is that the cooling curve of first mixed refrigerant is easy to be complementary with cooling curve first-class and second stream.U.S. Pat 6,272,882 have instructed and have used two kinds of mixed refrigerant components (promptly lighter gaseous state part and heavier liquid part), and this can be through separating the refrigerant stream of partial condensation in separation container and being controlled.The overall composition that changes such mixed refrigerant is very difficult and time-consuming with the component separately of changing light refrigerant part and heavier refrigerant part.
By contrast, the invention enables the cooling curve of first mixed refrigerant to change through the temperature difference of controlling first mixed refrigerant.The cooling curve of single mixed refrigerant component can be optimised, with first-class and second stream the cooling curve precision-matched.
Fig. 1 shows first embodiment of equipment 1, and this equipment is used to implement hydrocarbon stream 50 is cooled off the method with second stream of cooling that hydrocarbon stream 60 forms that are cooling are provided.This equipment comprises that 100, the first refrigerant loops, the first refrigerant loop comprise the refrigerant storage of first mixing.The first refrigerant loop 100 comprises first compressor 105 and is used for the compressive flow from first compressor 105 is effluented one or more first cooler 115a that (effluent stream) 110 cool off to 115c.Outflow stream from last first cooler (is 115c at this) is first refrigerant stream 120 of compression.
The equipment of Fig. 1 also comprises first heat exchanger 125.First heat exchanger 125 arranges that first refrigerant stream 120 that is used for first-class (for example be second refrigerant and flow 220 forms) and compression cools off, and per share flow point other places are in pipe side 221,121.Cooling medium is formed by first refrigerant stream 140 that first in the shell-side of first heat exchanger 125 expands.At the cold end place of first heat exchanger 125, be useful on the outlet of first-class (second refrigerant stream 230 that for example is cooling) that one cooling at least is provided, and the outlet that is useful on first refrigerant stream 130 of first cooling.Place, warm end or near, be useful on the outlet of first first refrigerant stream 150 that warms up.First expansion gear 135 is arranged the 130a of first of the first freezing stream 130 that is used to receive first cooling, and first first refrigerant stream 140 that expands is offered the shell-side of first heat exchanger 125.
This equipment also comprises second heat exchanger 145; This second heat exchanger is arranged first-class cooling that is used for cooling; This cooling first-class can be the second portion 130b of first refrigerant stream 130 of second refrigerant stream 230, hydrocarbon stream 50 and first cooling of cooling, and per share flow point other places are in pipe side 231,51,131.Cooling medium is formed by first refrigerant stream 170 that second in the shell-side of second heat exchanger 145 expands.Cold end place at second heat exchanger 145; Be useful on the outlet of the hydrocarbon stream 60 that cooling is provided at least; Be useful on the outlet of first-class (the second main refrigerant stream 240 that for example is another cooling) of another cooling, and the outlet that is useful on first refrigerant stream 160 of further cooling.Place, warm end or near, be useful on the outlet of second first refrigerant stream 180 that warms up.First expansion gear 165 is arranged the first of first refrigerant stream 160 that is used for receiving at least further cooling, and second first refrigerant stream 170 that expands is offered the shell-side of second heat exchanger 145.
Hydrocarbon stream 50 is one (first strands) that flow in one or multiply second stream of one or more second heat exchangers 145.Hydrocarbon stream 50 is fed into the second heat exchanger hydrocarbon stream pipe 51 in second heat exchanger 145, and at this place, it can carry out indirect heat exchange through the refrigerant that mixes with first of low pressure in the shell-side of second heat exchanger 145 evaporation and be cooled.Preferably, hydrocarbon stream 50 can be by partial condensation in second heat exchanger 145.
(preferred partial condensation) hydrocarbon of cooling flows out second heat exchanger 145 as the hydrocarbon stream 60 of cooling, and the hydrocarbon stream of this cooling is second stream of cooling.First refrigerant that mix can be the pre-cooled refrigerant in the pre-cooled refrigerant loop, is described in more detail below the operation to first refrigerant that mix.
Arranging of Fig. 1 also discloses the cooling to another second stream (second refrigerant stream 230 that for example, is cooling) and one or more first-class (for example, comprising second refrigerant stream 220).It is especially useful cooling off for second refrigerant that mix in this disclosed method, and this second refrigerant of mixing is used in the second cooling stage (not shown) the further cooling and preferred liquefaction of hydrocarbon stream 60 to cooling.The embodiment that combines Fig. 2 is described the second such cooling stage in more detail.
The refrigerant of second mixing preferably is cooled, and more preferably in two stages, carries out partial condensation.The refrigerant of second mixing can flow through one or two in first heat exchanger 125 and second heat exchanger 145 in first cooling stage.
First refrigerant that mix can flow in second heat exchanger 125, and to flow one (first) of 220 forms first-class as being second refrigerant.In the second refrigerant pipe 221 of first heat exchanger 125, second strand of second refrigerant that mixes is through carrying out indirect heat exchange with first refrigerant that mixes that in the shell-side of first heat exchanger 125, under middle pressure, evaporates and under elevated pressure, being cooled.The refrigerant that second of cooling mixes flows first-class first heat exchanger 125 that leaves of the cooling of 230 forms as second refrigerant that is cooling.
Second refrigerant stream 230 of cooling can be used as (the second) second stream 230 and flows to second heat exchanger 145.In second second refrigerant pipe 231 of second heat exchanger 145; The refrigerant stream that second of cooling mixes is through carrying out indirect heat exchange with first refrigerant that in the shell-side of second heat exchanger 145, under low pressure evaporates and under elevated pressure, being further cooled, preferably by partial condensation.Second refrigerant of another cooling flows as second of (second) cooling and leaves second heat exchanger 145, and second stream of this cooling can present the form of the second main refrigerant stream 240 of another cooling.Second refrigerant stream 240 of another cooling can flow to the main heat exchanger (not shown) then, so that cooling to be provided.
Get back to the first refrigerant loop, first of the evaporation refrigerant that mix is approximately removing from this under the middle pressure level as the first refrigerant stream 150 that warms up under middle pressure in the shell-side of first heat exchanger 125.First first refrigerant stream 150 that warms up can flow to the first baffle-type knockout drum (knock out drum) 155; To remove any liquid phase; Afterwards, first refrigerant stream 150 that the gaseous component of first first refrigerant stream 150 that warms up is warmed up as first of gaseous state ' and flow to first compressor 105.
The heat of compression together with from first-class and second stream (for this; Can use 120,50, among the 130b, 230 any) and first refrigerant stream 120 of compression at least a portion in the heat that absorbs be removed through using one or more first cooling devices 115 (such as ambient air cooler 115a, 115b), flow 114a, 114b with first refrigerant that (first) and (second) cooling is provided and compress respectively.The major part that is present in the heat in the compressive flow 110 is from as absorbing first second refrigerant stream 220 and second refrigerant stream 230 as the cooling of second stream.
(the second) first refrigerant stream 114b of cooling and compression is depicted as and flows to the first refrigerant memory 117.The first refrigerant memory 117 also can be formed stream 116 by one or more refrigerant components and supply with.Fig. 1 shows first and forms stream 116a, 116b with second first refrigerant component, and it can replenish the component that removes or reveal in the first refrigerant storage from the first refrigerant loop 100.First component and the second components selection property interpolation then can change the component of first mixed refrigerant.In order to keep the stabilized quality balance of the refrigerant that first in the first refrigerant loop mix, the first refrigerant discharge currents can be set.Instance among the embodiment as seen in fig. 1, first refrigerant can be removed via the first refrigerant discharge currents 119 from first refrigerant stream 114a of (first) cooling and compression.If remove than light component and heavier component in the first mixed refrigerant storage of expectation from the first refrigerant loop 100, then this is preferred.
In an alternate embodiments (not shown in Fig. 1), one or more first refrigerant discharge currents can remove from the first refrigerant memory 117.If the first refrigerant discharge currents, then can remove the light gaseous component of the refrigerant of first mixing according to qualifications from the top of memory 117.If the first refrigerant discharge currents be in memory 117 the bottom or near, then can remove the liquid composition of the weight of first refrigerant that mix according to qualifications.Thus, possibly regulate the component of the refrigerant of first mixing.
The refrigerant of first mixing can be discharged from as the first refrigerant incoming flow 118 from the first refrigerant memory 117, and this first refrigerant incoming flow can be cooled in cooling device (such as ambient cooler) 115c, so that first refrigerant stream 120 of compression to be provided.
First refrigerant stream 120 of compression is first-class and flow to first heat exchanger 125 as (second).(second) first-class pipe 121 that first refrigerant stream 120 of compression flows through in first heat exchanger 125, therein, first refrigerant of this compression stream is cooled, so that first refrigerant stream 130 of first cooling to be provided.
First refrigerant stream 130 of first cooling for example through using current divider (such as T shape pipe) to be divided into 130a of first and second portion 130b, keeps the component of first and second portion identical with the component of first refrigerant stream 130 of first cooling.The 130a of first of first refrigerant stream 130 of first cooling flows through first expansion gear (such as the form that is Joule-Thomson valve) 135, flows to the cold end of the shell-side of first heat exchanger 125, at this place, makes it under the middle pressure level, evaporate.First refrigerant of evaporation extracts heat from two first-class (first refrigerant stream, 120 and second refrigerant streams 220 of compression) flowing through pipe 121 and 221.
The remainder of first refrigerant stream 130 of first cooling (i.e. the second portion 130b of first refrigerant stream 130 of first cooling) flows to second heat exchanger 145.Second portion 130b flows in second the first refrigerant pipe 131 that is arranged in second heat exchanger 145, and at this place, this second portion is cooled so that first refrigerant stream 160 of further cooling to be provided.
Further first refrigerant of cooling stream 160 flows to second expansion gear (such as the form that is Joule-Thomson valve) 165, so that first refrigerant stream 170 of second expansion to be provided.Second first refrigerant stream 170 that expands is in than first first refrigerant that expand and flows under the 140 low pressure.First refrigerant stream 170 of second expansion flows to the cold end of the shell-side of second heat exchanger 145, at this place, makes it under low pressure evaporate.First refrigerant of evaporation flows from flowing through second of pipe 51 and 231 in (for example, second refrigerant stream 230 of hydrocarbon stream 50 and/or cooling) and extracts heat, and from the second portion 130b that manages first refrigerant stream 130 that cools off first 131, extracts heat.
Low refrigerant pressure down first refrigerant that mixes of evaporation flow 180 and from the shell-side of second heat exchanger 145, remove as second first refrigerant that warm up.Second first refrigerant stream 180 that warms up can flow to second baffle formula knockout drum 185, with first refrigerant stream 180 that warms up with gaseous state second at the gaseous component that makes second first refrigerant stream 180 that warms up ' form remove any liquid phase before flowing to first compressor 105.In two-stage compressor 105, the refrigerant of first mixing can be compressed to elevated pressure, so that compressive flow 110 to be provided.
Be apparent that one or more first coolers 115 can be water cooler rather than aerial cooler, if necessary, also can be by if replenish with the heat exchanger of another cooling agent.First expansion gear 135 and/or second expansion gear 165 can be substituted or replenished by expansion turbine.First heat exchanger 125 and second heat exchanger 145 can independently be selected from reel (spool wound) formula heat exchanger or flange plate type heat exchanger, although foregoing description is specifically described with reference to the roll type heat exchanger.
In an alternative embodiment, hydrocarbon stream can cool off in first heat exchanger and second heat exchanger.For example, Fig. 2 discloses a kind of equipment (line-up), and it comprises two all (just first with second) first heat exchanger 125a of operation, 125b and one second heat exchangers 145 of operation under low pressure under middle pressure.
Hydrocarbon incoming flow 20 is provided and flows to second first heat exchanger 125b, and at this place, it is cooled.Hydrocarbon incoming flow 20 is preferably by preliminary treatment, so that remove not desired components, for example sour gas will be described further below.In a preferred embodiment, second first heat exchanger 125b can be used for isolating any (remaining) water that is present in the hydrocarbon incoming flow 20.
Hydrocarbon incoming flow 20 can be present in the first heat exchanger hydrocarbon stream pipe 21, and first refrigerant that mixes that relies under the middle pressure in the shell-side of second first heat exchanger 125b is cooled.Second first heat exchanger 125b can be still formula heat exchanger, roll type heat exchanger or flange plate type heat exchanger according to expectation.The refrigerant that making wins mixes is along with its cooling hydrocarbon incoming flow 20 and evaporate, second strand of first first refrigerant stream 150b that warms up to be provided and as the hydrocarbon incoming flow 30 of the first cooling of cooling off.
Second strand of first first refrigerant stream 150b that warms up provides by second strand of first first refrigerant stream 140b that expands and by the third part 130c that flows through (second) first expansion gear 135b of first refrigerant stream 130 of first cooling, and this first expansion gear for example is Joule-Thomson valve or turbine expander.
First refrigerant stream, 130 conducts of first burst of cooling provide from first cool stream of various heat exchange device, and in this case, first first heat exchanger 125a can be coil exchanger or flange plate type heat exchanger.
First the first heat exchanger 125a is to cool off with first refrigerant stream 120 of the similar mode of the embodiment of Fig. 1 to one first-class (form that is second refrigerant stream 220) and compression.
Thereby, in the described equipment of Fig. 2, provide two first-class, hydrocarbon incoming flow 20 and second refrigerant stream 220, these two first-class cools off in the first independent heat exchanger 125a, 125b.
In this case, after cooling, first strand first first refrigerant stream 150a that warms up provides from the shell-side of first the first heat exchanger 125a.150b is combined for this first refrigerant that can warm up with (second strand) first from second first heat exchanger stream, and flows to the suction inlet in the middle pressure stage of first compressor 105.
Get back to the hydrocarbon incoming flow 30 of the cooling that is provided by second first refrigerant heat exchanger 125b, it can flow to natural gas liquids (NGL) recovery tower 45, for example fractionating column or scrubbing tower; For example; Be the form of domethanizing column, it provides liquid bottom stream, for example from tower bottom place or near natural gas liquids stream 40; And the cat head gaseous flow is provided, this cat head gaseous flow is a hydrocarbon stream 50.
In second heat exchanger 145 with the similar mode of the embodiment of Fig. 1 with the second portion 130b of first refrigerant stream 130 of first cooling to cooling off as the hydrocarbon stream 50 of second stream and as second refrigerant stream 230 of the cooling of another second stream.
The hydrocarbon stream 60 of cooling is second stream of the cooling that provided by second heat exchanger 145, and it can flow to first separator 65.First separator 65 provides the form that is methane rich overhead stream 70 bottom a part of and poor methane of the hydrocarbon stream 60 of cooling to flow 80.The bottom stream 80 of this poor methane can be used as Modelling of Flow with Recirculation to NGL recovery tower 45.The bottom stream 80 of poor methane can at first be transported to the baffle-type gas-liquid separator (not shown) of backflow, to remove the gaseous state part.The liquid part of the bottom stream of poor methane is pressurizeed by reflux pump 75 then, so that (pressurization) poor methane bottom stream 80a to be provided, should can supply to NGL recovery tower 45 under the tower operating pressure or under the pressure of a little higher than this pressure by (pressurization) poor methane bottom stream 80a.
The bottom stream 80 of poor methane can turn back to the top part of fractionating column 45.Through before separating at first separator 65 in second heat exchanger 145 hydrocarbon stream 50 of this cooling of cooling, reflow stream can with do not carry out being provided under the lower temperature of this pre-cooled apparatus in comparison.The temperature of this backflow has confirmed to supply to the temperature upper limit of hydrocarbon stream 60 of the cooling of NGL recovery tower 45.This allows to provide technology more efficiently, because the methane-rich stream 70 of extracting out from the top of NGL recovery tower 45 can be cooled under lower temperature, preferably by partial condensation.As a result, the temperature at the cold end place of second heat exchanger 145 can be lower.Thereby the temperature that the refrigerant of first mixing is cooled to is lower, and this has caused the low cycling rate of refrigerant.
Methane-rich stream 70 can flow to one or more main heat exchangers 85 then; In this main heat exchanger, its can in the methane-rich stream pipe 71 of main heat exchanger, rely on second refrigerant in the shell-side of main heat exchanger 85 and be cooled and at least in part (fully preferred) be liquefied.Second refrigerant can be the refrigerant that mix in second in the second refrigerant loop, and its operation is known to those skilled in the art.An instance operating second refrigerant can find in US patent 6,370910.
This at least the pressure of the hydrocarbon stream 90 of part (fully preferred) liquefaction can in terminal flash distillation expansion gear (such as Joule-Thomson valve and/or expander) 87, be lowered, with the hydrocarbon stream 91 that expansion is provided.
The hydrocarbon stream 91 that expands can flow to terminal flash separator 95, so that terminal flash streams 97 and liquefied hydrocarbon product stream 99 to be provided.
In a preferred embodiment, when hydrocarbon incoming flow 20 is natural gas flow, liquefied hydrocarbon product stream 99 will be LNG stream.
The method and apparatus that is used to cool off described herein can use advanced process controller to control.Employed model is confirmed one group of Synchronization Control behavior of controlling variable based on PREDICTIVE CONTROL in controller, thereby at least one control variables of control or one group of control variables, optimizes at least one parameter in one group of parameter will optimizing.
Control variable and comprise for this group:
The component of the refrigerant storage that mix in first in-the first refrigerant loop 100,
The setting of-the first expansion gear 135, and
The setting of-the second expansion gear 165.
In first expansion gear 135 and second expansion gear 165, advanced process controller can be given the minimum more weights of equipment of pressure variation between both sides valuably, so that it provides the minimum temperature of the refrigerant of first mixing to reduce.
Can be to the setting of first expansion gear 135 and second expansion gear 165 through changing by the actuator of controlling from the control signal of advanced person's process controller.Sort controller also can with actuator configurations first discharge currents and one or more first refrigerant component constitute in the stream one or more on, adjust the component of the refrigerant storage of mixing in first in the first refrigerant loop 100 via control signal.
As above discussed, any controlling of the component of the refrigerant storage of first mixing can be realized via the first refrigerant memory 117.Yet; Be important to note that; Although the component of the refrigerant storage that mix in first in the first refrigerant loop 100 can be changed, first refrigerant of compression flows in 120 and first first refrigerant that warms up stream 150 is identical with the component that second first refrigerant that warms up flows the refrigerant storage of first mixing among or preferred two in 180.Preferably, it is identical with the component that first refrigerant that flows through second expansion gear 165 flows to flow through the component of first refrigerant stream of first expansion gear 135.
This group of control variables comprises one or more in following group:
The temperature of at least one in second stream of-one or multiply cooling (form of the second main refrigerant stream 240 that for example is hydrocarbon stream 60 and/or another cooling of cooling) is preferably the temperature of the hydrocarbon stream 60 of cooling,
Temperature difference between at least a in-the first first refrigerant stream 150 that warms up and the following stream: (i) first refrigerant of compression stream 120 and (ii) first-class (for example be the hydrocarbon incoming flow 20 and/or second refrigerant and flow 220 form),
Temperature difference between at least a in-the second first refrigerant stream 180 that warms up and the following stream: (i) a kind of in the second portion 130b of first refrigerant stream 130 of first cooling and (ii) one or more second the flowing of form that are first-class (second refrigerant stream 230 of the hydrocarbon incoming flow 30 of cooling and/or cooling) of cooling and/or are derived from first-class 30 stream (it is called as " attached stream ") of cooling (for example being the form that flows in 30,50,230 any)
In the following control variables at least one: (i) temperature difference between first refrigerant stream 170 of first refrigerant stream, 160 and second expansion of temperature difference between first refrigerant stream 140 of first refrigerant stream, 130 and first expansion of first cooling and (ii) further cooling, and
-the power that consumes by one or more first compressors 105.
Second above-mentioned control variables and the 3rd control variables manage to limit the variations in temperature between one at least in the stream of first refrigerant that warms up that flows out first heat exchanger and second heat exchanger and the warm end of this heat exchanger of entering.
About the second above-mentioned control variables, the temperature difference between one at least in the stream of having confirmed to locate first first refrigerant stream, 150 and first heat exchanger, the 125 warm ends that warm up.The said stream at the place, warm end of first heat exchanger 125 can be selected from and comprise that first-class first refrigerant with compression flows 120 group.The first-class group that can preferably be selected from second refrigerant stream 22 that comprises in the hydrocarbon incoming flow 20 (like what discussed among Fig. 2) and the second refrigerant loop (not shown).Preferably, cause the combination of these streams of minimum temperature difference to be used as control variables and given big relatively weight.
About the 3rd above-mentioned control variables, the temperature difference between one at least during these of place, warm end of having confirmed second first refrigerant stream, 180 and second heat exchanger 145 that warm up flow.First-class 30,230 and/or one group from one or multiply second stream of the form of the first-class attached stream that derives of cooling (its can be used for these streams 30,50,230 one or more) that the said stream at the place, warm end of second heat exchanger 145 can be selected from the second portion 130b of first refrigerant stream 130 that comprises first cooling and be cooling.Preferably, cause the temperature difference of combination of these streams of minimum temperature difference to give big relatively weight as control variables.
Confirm that first needed temperature and temperature difference in above-mentioned four control variables can measure through the temperature sensor that is used for monitoring the related streams temperature.Temperature sensor can be sent to advanced process controller with temperature sensor signal, and this controller is carried out said control method.In response to temperature signal, control signal can for example be sent to and be used for that expansion gear and/or first refrigerant are discharged and component is replenished the actuator of stream, controls one or more in the variable so that change.Similarly, the power demand of one or more first compressors can be measured through the sensor in one or more compressors or corresponding one or more first compressor apparatus, and is sent to advanced process controller.
One group of parameter optimizing comprises productivity ratio and/or the cooling effectiveness in the first refrigerant loop of the hydrocarbon stream of cooling.
The productivity ratio of the hydrocarbon stream of cooling can be confirmed through for example use traffic sensor measurement mass flowrate or correlation properties.The cooling effectiveness in the first refrigerant loop can calculate through known technology, and this known technology is based on the power demand of first compressor As time goes on and the relation of the amount of the hydrocarbon stream 60 of the cooling of being produced.
The key character of Model Predictive Control is: following behavior is through using a model and effective measurement of control variables is predicted.As in Perry ' s Chemical Engineers ' Handbook, 7
ThEdition; Further explain among the page 8-5 to 8-27; It is incorporated in this paper by reference, and the output of computing controller is so that be optimized performance indications, and these performance indications can be the linearity or the quadratic functions of predicated error and the control progress of being calculated in future (moves).In each sampling instant, repeat control and calculate, and upgrade this prediction based on current measurement.Suitable model is a kind of one group of empirical formula step response model having represented the step response effect of controlling variable on control variables that comprises.
Want the optimum value of optimum parameters to obtain from independent optimization step, the variable that perhaps will optimize can be included in the performance function.
Before can the application model PREDICTIVE CONTROL, the step of at first confirming to control variable changes to the influence of the variable that will optimize and to the influence of control variables.This operation provides one group of step-response coefficients.This group step-response coefficients has formed the basis of the Model Predictive Control of cooling procedure.
At normal operation period, the predicted value of control variables is carried out well-regulated calculating for the control progress in many future.Then, can calculate the performance indications that are used for these control progress in the future.These performance indications can comprise two projects, and first project representes to be used for the summation that future, control made progress of each predicated error of controlling progress, and second project representes to be used for the summation of each control in the future of controlling the variation of controlling variable that makes progress progress.
For each control variables, predicated error is the difference between the reference value of predicted value and control variables of control variables.Predicated error multiply by weighted factor, and the progression inhibiting factor is multiply by in the variation of controlling variable that is used to control progress.In this case, performance indications will be linear.Alternately, project can be the project quadratic sum, and in this case, these performance indications are secondaries.
Variation and the control variables of can control variable to these, controlling variable are provided with constraints.This has caused independently one group of equality, and these equalities are found the solution through performance indications are minimized simultaneously.
When carrying out optimization independently, can comprise and want optimum parameters that with the control variables as the predicated error that is used for each control progress, and this optimization provides the reference value of control variables.
Alternately, in the computer capacity of performance indications, be optimized, and this be the 3rd project in the performance indications given weighted factor suitably.In this case, the reference value of control variables is the predetermined steady-state value that keeps constant.
Consider that constraints minimizes performance indications, think that in the future control progress is given to control variate-value.But, only carry out ensuing control progress.Then, restart the calculating of the performance indications of progress in the future.
Model with step-response coefficients can be the part of computer program with the equality that is used for Model Predictive Control, and this program is performed to control this cooling procedure.But the computer that is mounted with the program of this transaction module PREDICTIVE CONTROL is called as advanced process controller.The base program bag that lacks particular model PREDICTIVE CONTROL disclosed herein be can obtain from market and be known to those skilled in the art.Method and apparatus described here benefit to the useful selection of the setting of controlling variable and control variables.
For example; In one embodiment; When first refrigerant that mix comprises methane, ethane and propane at least, in the first refrigerant loop 100, comprise the controlling variable and can comprise in methane, ethane and the propane content of controlling in the first refrigerant storage one or more of component of the first refrigerant storage of mixing.
Method and apparatus described here any hydrocarbon stream that can be used for liquefying, but be desirably in the natural gas liquefaction particularly useful, so that liquefied natural gas (LNG) to be provided.
Thereby hydrocarbon stream can be arbitrary suitable air-flow that will be cooled and be liquefied alternatively, but suitably is the natural gas flow that obtains by in natural gas or the oil gas reservoir.As a kind of replacement scheme, natural gas flow also can obtain from other source, also comprises synthetic source, such as fischer-tropsch process.
Usually, natural gas flow is the hydrocarbon component that mainly comprises methane.Preferably, the hydrocarbon incoming flow comprises the methane of 50mol% (molar percentage) at least, more preferably comprises the methane of 80mol% at least.
Hydrocarbon component (such as natural gas) also can comprise non-hydrocarbons, such as H
2O, N
2, CO
2, Hg, H
2S and other sulfide or the like.If expectation, natural gas can carry out preliminary treatment before cooling and any liquefaction.This preliminary treatment can comprise reduction and/or remove not desired components, (such as CO
2And H
2S) or other steps (for example cooling, precharge etc. in early days).Because these steps are known to those skilled in the art, no longer discuss their mechanism at this.
Therefore; Term " hydrocarbon stream " also can be included in the component before any processing; Said processing comprises cleaning, dehydration and/or dedusting; And for reduce and/or remove one or more mixtures or material and by part, basically or any component of all handling, it includes, but are not limited to: sulphur, sulphur compound, carbon dioxide, water, mercury and one or more C
2+Hydrocarbon.
According to the source, natural gas can comprise the hydro carbons of the variable quantity heavier than methane, for example especially ethane, propane and butane, and maybe more a spot of pentane and aromatic hydrocarbons.This component changes according to the type and the occasion of gas.
Traditionally, because a variety of causes for example has the different freezing or condensing temperature of the each several part that can cause its obstruction methane liquefaction equipment, the hydrocarbon heavier than butane removed before carrying out any remarkable cooling as far as possible efficiently.Through domethanizing column, C
2+Hydrocarbon can be isolated from the hydrocarbon incoming flow, and their content in the hydrocarbon incoming flow is reduced, and this will provide the top hydrocarbon stream of methane rich and comprise most C
2+The bottom poor methane stream of hydrocarbon.The stream of bottom poor methane can flow in another separator then, so that liquefied petroleum gas (LPG) and condensate flow to be provided.
At after separating, the hydrocarbon stream that is produced can be cooled.This is for example as stated shown in the circuit in Fig. 2 50.Can this cooling be provided through a lot of methods known in the art, comprise so-called pair of mixed refrigerant (DMR) technology, for example but be not restricted to aforesaid technology and the technology described in following patent for example: US 5,826, and 444; US 6,041, and 619; US 6,105, and 389; US 7,096, and 688; US 6,370, and 910; WO 2008/009721; WO2008/019999; WO 2008/043806; WO 2009/007435, and comprises so-called single mixed refrigerant (SMR) technology, for example but be not limited to the illustrated technology of for example following patent: US6,041,619; US 6658891; US 5832745.Hydrocarbon stream flows through against the one or more refrigerant streams in one or more refrigerants loop.This refrigerant loop can comprise one or more compressors, and the refrigerant that at least partly evaporates with compression flows, thereby the refrigerant stream of compression is provided.The refrigerant stream of compression can be cooled in cooler (such as air or water cooler) then, so that refrigerant stream to be provided.This compressor also can be driven by one or more turbines.
The cooling of hydrocarbon stream can realize in one or more stages.Initial cooling is also referred to as pre-cooled or auxiliary cooling, can in two or more pre-cooled heat exchangers, carry out by the pre-cooled mixed refrigerant through pre-cooled refrigerant loop, so that the hydrocarbon stream of cooling to be provided.The hydrocarbon stream preference of cooling is as being lower than under zero ℃ the temperature by partial liquefaction.
Preferably, this pre-cooled heat exchanger can comprise the pre-cooled stage, wherein in one or more main heat exchangers, carries out any cooling subsequently, liquefies with the part to hydrocarbon stream in the cooling stage of one or more masters and/or secondary cooling.
First heat exchanger of being discussed in the above-described embodiments and second heat exchanger can be this pre-cooled heat exchangers in the pre-cooled stage, and first mixed refrigerant can be pre-cooled mixed refrigerant.
Thus, can comprise two or more cooling stages in this disclosed method, each stage has one or more steps, part etc.For example, each cooling stage can comprise one to five heat exchanger.The part of hydrocarbon stream or hydrocarbon stream and/or the refrigerant that mixes can not flow through all heat exchangers of cooling stage and/or the heat exchanger that all are identical.
In one embodiment, the hydrocarbon cooling procedure can comprise single cooling stage.In another embodiment, hydrocarbon can cool off in the method that comprises two or three cooling stages and liquefy.The pre-cooled stage is preferably used for temperature with the hydrocarbon incoming flow and is reduced to and is lower than 0 ℃, usually in-20 ℃ to-70 ℃ scope.
Main cooling stage preferably separates with the pre-cooled stage.That is to say that main cooling stage comprises one or more independent main heat exchangers.Main cooling stage can be frozen through using above-mentioned second refrigerant stream.
Main cooling stage is preferably used for temperature with hydrocarbon stream (the normally part of the hydrocarbon stream through the cooling of pre-cooled stage) and is reduced to and is lower than-100 ℃.
As two or more pre-cooled heat exchangers or any main heat exchanger is known in the art.Pre-cooled heat exchanger is shell-and-tube heat exchanger preferably.
In all these main heat exchangers at least one roll type cryogenic heat exchanger preferably as known in the art.Alternatively, heat exchanger can comprise the one or more cooling end sections that are in its enclosure interior, and each cooling end section can be considered to a cooling stage or be considered to " heat exchanger " independent with respect to another cool position.
In another said embodiment; In the main refrigerant stream of the pre-cooled refrigerant stream that mixes and arbitrary mixing one or two can flow through one or more heat exchangers; Preferably flow through in above-mentioned pre-cooled and the main heat exchanger two or more, with the refrigerant stream of mixing that cooling is provided.
The refrigerant of the mixing in the refrigerant loop of mixing (for example the refrigerant loop in first (for example pre-cooled) or arbitrary main refrigerant loop) can form by being selected from two kinds of comprising in the following group or the mixture of more kinds of components: nitrogen, methane, ethane, ethene, propane, propylene, butane, pentane or the like.The present invention can be included in refrigerant separation or overlapping loop or other cooling circuits and to use one or more other refrigerant.
As comprising two kinds of different components of 5mol% at least at the refrigerant of this pointed mixing or the refrigerant stream of mixing.More preferably, the refrigerant of mixing comprises two or more in the group that comprises following material: methane, ethane, ethene, propane, propylene, butane and pentane.For the refrigerant that mixes, common component can be:
Methane (C1) 0-20mol%;
Ethane (C2) 5-80mol%;
Propane (C3) 5-80mol%;
Butane (C4) 0-15mol%;
Total component comprises 100mol%.
In another embodiment, the hydrocarbon stream of cooling (such as the natural gas flow of cooling) can be further cooled, with the hydrocarbon stream (such as LNG stream) that liquefaction is provided.
Preferably, the hydrocarbon stream of the cooling that is provided by said method and apparatus can be used for providing the hydrocarbon stream of liquefaction, and this hydrocarbon stream can be stored in one or more storage tanks.
After liquefaction, the hydrocarbon stream of liquefaction if necessary also can be by further processing.As an instance, the Liquefied Hydrocarbon that is obtained can reduce pressure by means of Joule-Thomson valve or by means of the cryogenic turbo decompressor.
In this disclosed another embodiment; The hydrocarbon stream of liquefaction flows through terminal gas/liquid separation device (such as the terminal flash vessel); So that terminal flash distillation top stream and liquid bottom stream to be provided, this liquid bottom stream is used for being stored in storage tank as liquiefied product alternatively, such as LNG.The terminal flash gas can be compressed in the flash gas compressor of terminal so that the terminal flash gas stream of compression to be provided; And can be cooled so that the terminal flash streams of cooling to be provided, the terminal flash streams of this cooling can flow to one or more combustion gas headers or export as combustible gas.
It will be understood by those skilled in the art that the present invention can realize with a lot of different modes under the situation of the scope that does not break away from accompanying claims.
Claims (15)
1. method of producing the hydrocarbon stream of cooling, said method comprises to be cooled off hydrocarbon stream, and this method may further comprise the steps at least:
(a) flow first refrigerant stream that cools off the compression in first-class and the first refrigerant loop through first refrigerant that under first stress level, in first heat exchanger, relies on first expansion; With first refrigerant stream that first refrigerant stream and first first-class, first cooling that cooling is provided warms up, this first refrigerant loop comprises the refrigerant that first compressor and first mixes;
(b) first to first refrigerant stream of first cooling expands in first expansion gear, so that first first refrigerant stream that expands to be provided;
(c) second portion of first refrigerant stream through in second heat exchanger, relying on second first refrigerant that expand to flow to cool off one or multiply second stream and first cooling; Flow with second stream that provides one or multiply to cool off, first refrigerant that first refrigerant stream and second of further cooling warms up; Wherein, Said one or multiply second flow to and comprise the first-class of said cooling less and by the first-class attached stream of deriving of said cooling; Hydrocarbon stream is comprised in said one or multiply second stream, so that the hydrocarbon stream of said cooling to be provided at least thus;
(d) in second expansion gear, the first at least of first refrigerant of said further cooling stream is expanded; So that first refrigerant stream of second expansion to be provided; First refrigerant stream of said second expansion is in than under the low pressure of first refrigerant stream of said first expansion, and
The gaseous state of first refrigerant stream that (e) in first compressor, said first first refrigerant stream and said second that warms up is warmed up partly compresses, and then the compressive flow from first compressor is cooled off, and flows with first refrigerant that compression is provided;
Said method also comprises the steps: through using based on the Advanced process control device of Model Predictive Control step (a) to (e) to be controlled; To confirm for one group of Synchronization Control behavior of controlling variable; So that at least one in one group of control variables of control at least one parameter in one group of parameter will optimizing is optimized, controls variable and comprise for wherein said one group:
The component of the refrigerant storage that mix in first in-the first refrigerant loop,
The setting of-the first expansion gear and
The setting of-the second expansion gear,
Wherein said one group of control variables comprises:
One temperature at least in second stream of-said one or multiply cooling,
Temperature difference between at least a in-said first first refrigerant stream that warms up and the following stream: (i) first refrigerant of said compression stream and (ii) said first-class,
Temperature difference between at least a in-said second first refrigerant stream that warms up and the following stream: (i) second portion of first refrigerant stream of said first cooling and (ii) be the first-class of said cooling and/or from said one or the multiply second of the form of the first-class attached stream of deriving of said cooling flows one
In-following the control variables at least one: the temperature difference between first refrigerant stream that the temperature difference between (i) first refrigerant of first refrigerant stream of first cooling and first expansion flows and first refrigerant stream and said second of (ii) said further cooling expand, and
-the power that consumes by first compressor;
And; The said one group of parameter that wherein will optimize comprises productivity ratio and/or the cooling effectiveness in the first refrigerant loop of the hydrocarbon stream of cooling, and said cooling effectiveness has reflected the relation of the power that As time goes in first compressor, consumes and the amount of the cooling hydrocarbon stream that is produced.
2. the method for claim 1; Wherein, Said first refrigerant that mix comprises methane, ethane and propane at least, the component of said first refrigerant that mix is controlled comprise one or more in methane, ethane and the propane storage of controlling first mixed refrigerant in the first refrigerant loop.
3. like each described method in the aforementioned claim; Wherein, Saidly first-classly comprise the hydrocarbon incoming flow, thus the first-class hydrocarbon incoming flow that comprises cooling of said cooling, and said one or multiply second stream comprise the hydrocarbon incoming flow of cooling or by the first-class attached stream of deriving of said cooling.
4. method as claimed in claim 3 also comprises: in step (c) before, and through in the natural gas liquids recovery tower, the hydrocarbon incoming flow being carried out fractionation and from said cooling first-class, derive hydrocarbon, so that hydrocarbon stream and liquid bottom stream to be provided.
5. like each described method in the above-mentioned claim; Wherein, Said first-class second refrigerant stream that comprises the refrigerant that mix in second in the second refrigerant loop; Said cooling first-class comprises second refrigerant stream of cooling thus, and said one or multiply second stream comprise second refrigerant stream and the hydrocarbon stream of cooling, and second stream of said one or multiply cooling comprises second refrigerant stream of another cooling and the hydrocarbon stream of cooling.
6. each described method as in the above-mentioned claim wherein comprises two strands or more multiply is first-class in the first identical heat exchanger or per share first-classly in independent high pressure first heat exchanger, cool off to first-class the cooling.
7. each described method as in the above-mentioned claim, wherein to said one or multiply second stream cool off comprise to two strands or more multiply second stream cool off in the second independent heat exchanger at second identical heat exchanger or per share second stream.
8. like each described method in the above-mentioned claim, further comprising the steps of:
(h) in main heat exchanger, at least a portion in the hydrocarbon stream of said cooling is carried out partial liquefaction at least, preferably liquefy fully.
9. the method described in claim 8, further comprising the steps of:
(f) in first separator, isolate the hydrocarbon stream of said cooling, with the part of the form of bottom stream that the overhead stream that is methane rich and poor methane are provided; And alternatively,
(g) the bottom stream to poor methane pressurizes, and flows so that (pressurization) poor methane bottom to be provided, and makes the bottom stream of said (pressurization) poor methane flow to the natural gas liquids recovery tower as backflow.
10. like claim 8 or 9 described methods; Wherein, the part of the hydrocarbon stream of said cooling is carried out partial liquefaction at least, preferably liquefaction fully; Comprise: the methane-rich stream and second refrigerant are carried out heat exchange, so that the preferred hydrocarbon stream of liquefaction fully of part at least to be provided.
11. like claim 8 or 9 described methods; Wherein, Part to the hydrocarbon stream of said cooling is carried out part at least, and preferably liquefaction fully comprises: the second portion of the said part of the hydrocarbon stream of said cooling and first refrigerant stream of further cooling is carried out heat exchange; Partial liquefaction at least to be provided, the preferred hydrocarbon stream of liquefaction fully.
12., further comprising the steps of like each described method among the claim 8-11:
(i) reduce said partial liquefaction at least, the preferred pressure of the hydrocarbon stream of liquefaction fully is with hydrocarbon product stream and the terminal flash gas stream that liquefaction is provided.
13. like each described method in the above-mentioned claim, wherein said hydrocarbon stream is a natural gas flow.
14. like each described method in the above-mentioned claim, wherein, the component of the first that in step (b), is inflated is identical with the component at least partly that first refrigerant of the further cooling that in step (d), is inflated flows basically.
15. an equipment that is used for producing from hydrocarbon stream the hydrocarbon stream of cooling, said equipment comprises:
-the first refrigerant loop, the said first refrigerant loop comprise the refrigerant storage of first mixing; First expansion gear; Second expansion gear; First compressor; With one or more first coolers, said one or more first coolers cool off for the compressive flow from first compressor, thereby first refrigerant stream of compression is provided;
-the first heat exchanger; Said first heat exchanger is arranged and is used under first pressure, relying on first refrigerant of first expansion to flow first refrigerant stream to first-class and compression to cool off; With first refrigerant stream that first refrigerant stream and first first-class, first cooling that cooling is provided warms up, first expansion gear is arranged the first of first refrigerant stream that is used to receive first cooling and first first refrigerant stream that expands is provided;
-the second heat exchanger; Second heat exchanger is arranged and to be used to rely on second first refrigerant stream that expands that the second portion that first refrigerant of one or multiply second stream and first cooling flows is cooled off; Flow with second stream that provides one or multiply to cool off, first refrigerant that first refrigerant stream and second of further cooling warms up; Second expansion gear is arranged the first at least of first refrigerant stream be used to receive further cooling; So that first refrigerant stream of second expansion to be provided; First refrigerant stream of said second expansion is in than under the low pressure of first refrigerant stream of said first expansion; Said one or multiply second flow to and comprise the first-class of said cooling less or by the first-class attached stream that derives of said cooling, and hydrocarbon stream is included in said one or multiply second stream, so that the hydrocarbon stream of said cooling is provided at least thus;
-said first compressor arranges that the gaseous state that is used for first refrigerant that said first first refrigerant stream and said second that warms up warms up flows partly compresses;
-advanced process controller; Said process controller comprises based on the computer-executable code of Model Predictive Control confirms the Synchronization Control effect of controlling variable for one group; So that at least one in one group of control variables of control at least one parameter in one group of parameter will optimizing is optimized; Wherein, control variable and comprise for said one group:
The component of the refrigerant storage that mix in first in-the first refrigerant loop,
The setting of-the first expansion gear and
The setting of-the second expansion gear,
Wherein said one group of control variables comprises:
One temperature at least in second stream of-said one or multiply cooling,
Temperature difference between at least a in-the first first refrigerant stream that warms up and the following stream: (i) first refrigerant of compression stream and (ii) first-class,
Temperature difference between at least a in-the second first refrigerant stream that warms up and the following stream: (i) second portion of first refrigerant stream of first cooling and (ii) be the first-class of cooling and/or flow by one or multiply second of the form of the first-class attached stream of deriving of this cooling in one
In-following the control variables at least one: (i) temperature difference between first refrigerant stream of first refrigerant stream of temperature difference between first refrigerant stream of first refrigerant stream of first cooling and first expansion and (ii) further cooling and second expansion, and
-the power that consumes by first compressor;
And; One group of parameter wherein will optimizing comprises productivity ratio and/or the cooling effectiveness in the said first refrigerant loop of the hydrocarbon stream of said cooling, and said cooling effectiveness has reflected the relation of the power that As time goes in first compressor, consumes and the amount of the cooling hydrocarbon stream of being produced.
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| EP09164547.3 | 2009-07-03 | ||
| PCT/EP2010/059341 WO2011000900A2 (en) | 2009-07-03 | 2010-07-01 | Method and apparatus for producing a cooled hydrocarbon stream |
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| CN102472572B CN102472572B (en) | 2014-06-25 |
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|---|---|
| US (1) | US20120103011A1 (en) |
| EP (1) | EP2449325B1 (en) |
| JP (1) | JP5726184B2 (en) |
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| CN103542692B (en) * | 2012-07-09 | 2015-10-28 | 中国海洋石油总公司 | Based on the Unconventional forage liquefaction system of wrap-round tubular heat exchanger |
| BR112015009964A2 (en) * | 2012-11-16 | 2017-07-11 | Exxonmobil Upstream Res Co | hydrocarbon processing system, and method for the formation of a liquefied natural gas |
| JP6254614B2 (en) * | 2013-01-24 | 2017-12-27 | エクソンモービル アップストリーム リサーチ カンパニー | Liquefied natural gas production |
| MY190843A (en) * | 2016-03-10 | 2022-05-12 | Jgc Corp | Method of determining mixed refrigerant composition for natural gas liquefying apparatus |
| US10481018B2 (en) * | 2016-04-19 | 2019-11-19 | General Electric Company | Evaluating performance of a fluid transport system using limited sensor data |
| RU2645095C1 (en) * | 2017-04-03 | 2018-02-15 | Общество с ограниченной ответственностью "Научно-исследовательский институт природных газов и газовых технологий - Газпром ВНИИГАЗ" | Method of partial liquefaction of natural gas |
| US20200309450A1 (en) | 2017-12-07 | 2020-10-01 | Shell Oil Company | Compact lng production train and method |
| RU2020122328A (en) | 2017-12-07 | 2022-01-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | METHOD OF OPERATION OF A LIQUEFIED NATURAL GAS FACILITY |
| WO2021240689A1 (en) * | 2020-05-27 | 2021-12-02 | 千代田化工建設株式会社 | Method and system for determining operating conditions of liquefied natural gas plant |
| EP4537035A1 (en) * | 2022-07-04 | 2025-04-16 | Nuovo Pignone Tecnologie - S.R.L. | Gas liquefaction system with multiple refrigerant cycles |
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- 2010-07-01 AU AU2010268014A patent/AU2010268014B2/en active Active
- 2010-07-01 AP AP2011005998A patent/AP2991A/en active
- 2010-07-01 KR KR1020117031520A patent/KR20120093068A/en active Pending
- 2010-07-01 JP JP2012518904A patent/JP5726184B2/en active Active
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- 2010-07-01 NO NO10726536A patent/NO2449325T3/no unknown
- 2010-07-01 RU RU2012103560/06A patent/RU2537483C2/en active
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Also Published As
| Publication number | Publication date |
|---|---|
| KR20120093068A (en) | 2012-08-22 |
| DK180179B1 (en) | 2020-07-16 |
| CA2765476C (en) | 2017-10-24 |
| US20120103011A1 (en) | 2012-05-03 |
| RU2537483C2 (en) | 2015-01-10 |
| RU2012103560A (en) | 2013-08-10 |
| BR112012000045B1 (en) | 2020-09-08 |
| WO2011000900A3 (en) | 2011-04-14 |
| NO2449325T3 (en) | 2018-01-20 |
| JP2012531576A (en) | 2012-12-10 |
| AP2991A (en) | 2014-09-30 |
| AU2010268014B2 (en) | 2013-08-29 |
| BR112012000045A2 (en) | 2016-03-15 |
| AP2011005998A0 (en) | 2011-12-31 |
| EP2449325B1 (en) | 2017-08-23 |
| WO2011000900A2 (en) | 2011-01-06 |
| JP5726184B2 (en) | 2015-05-27 |
| EP2449325A2 (en) | 2012-05-09 |
| DK201170659A (en) | 2011-11-29 |
| CA2765476A1 (en) | 2011-01-06 |
| AU2010268014A1 (en) | 2011-12-22 |
| CN102472572B (en) | 2014-06-25 |
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